EP2906876B1 - Procédé de fonctionnement d'un générateur de vapeur - Google Patents

Procédé de fonctionnement d'un générateur de vapeur Download PDF

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Publication number
EP2906876B1
EP2906876B1 EP13777007.9A EP13777007A EP2906876B1 EP 2906876 B1 EP2906876 B1 EP 2906876B1 EP 13777007 A EP13777007 A EP 13777007A EP 2906876 B1 EP2906876 B1 EP 2906876B1
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EP
European Patent Office
Prior art keywords
lignite
mill
drying
dry
stream
Prior art date
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Not-in-force
Application number
EP13777007.9A
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German (de)
English (en)
Other versions
EP2906876A2 (fr
EP2906876B2 (fr
Inventor
Rainer Hesse
Bernhard Röper
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RWE Power AG
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RWE Power AG
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Application filed by RWE Power AG filed Critical RWE Power AG
Priority to PL13777007T priority Critical patent/PL2906876T5/pl
Publication of EP2906876A2 publication Critical patent/EP2906876A2/fr
Publication of EP2906876B1 publication Critical patent/EP2906876B1/fr
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K1/00—Preparation of lump or pulverulent fuel in readiness for delivery to combustion apparatus
    • F23K1/04—Heating fuel prior to delivery to combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2201/00—Pretreatment of solid fuel
    • F23K2201/20—Drying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2201/00—Pretreatment of solid fuel
    • F23K2201/50—Blending
    • F23K2201/501—Blending with other fuels or combustible waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2203/00—Feeding arrangements
    • F23K2203/002—Feeding devices for steam boilers, e.g. in locomotives
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2203/00—Feeding arrangements
    • F23K2203/20—Feeding/conveying devices
    • F23K2203/202—Feeding/conveying devices using screws
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2900/00—Special features of, or arrangements for fuel supplies
    • F23K2900/01041—Heating by using exhaust gas heat

Definitions

  • the invention relates to a method for operating a steam generator with a lignite-fired boiler, with at least one mill for grinding the brown coal.
  • a well-known principle of direct dust injection by means of a pulverized coal drying plant for example, in the Publication Helmut Effenberger, "steam generation", Springer-Verlag, ISBN 3-540-64175-0 , described.
  • the drying gas flue gas which is referred to in the sense of the present application as a drying flue gas stream.
  • the mill is connected via a flue gas recirculation to the end of the combustion chamber, where the drying flue gas stream required for drying the lignite coal is removed at a temperature between about 800 ° C and about 1200 ° C.
  • a method of the type mentioned is, for example, from DE 42 03 713 C2 C2 or from the DE 43 23 469 A1 known.
  • the process involves the milling of brown coal wet lignite in at least one mill, which is supplied with a drying flue gas stream, which is branched off from the boiler behind the convection train and is introduced into the mill at a temperature of about 350 ° C.
  • the brown coal is comminuted to the grain band required for combustion in the boiler and at the same time dried in the inert flue gas atmosphere.
  • Part of the drying flue gas stream is used as a carrier gas for transporting the dried fuel to the burners of the boiler. This combined predrying and grinding of lignite at a low temperature level is to be considered favorable in terms of the efficiency of the power plant.
  • Another variant of the drying of lignite which has a favorable effect in terms of an increase in efficiency, is the drying of lignite in a separate drying unit in the form of a fluidized bed dryer.
  • a separate drying unit in the form of a fluidized bed dryer.
  • Such a method is for example from the DE 196 20 047 A1 known. It is known that by drying the brown coal before burning in the Steam generator of a power plant, a significant increase in efficiency can be achieved.
  • the lignite brown coal has a water content of 45% to 65%, which is reduced by drying to 10% to 25%.
  • the dry lignite from the fluidized bed drying usually has a maximum water content of 25 percent by mass and a mean particle diameter D50 0.4 to 0.8 mm, so that it can be added directly, possibly without subsequent grinding in the boiler and burned there.
  • the combustion temperature of pre-dried lignite hereinafter referred to as dry lignite (TBK) is about 500 ° C higher than that of lignite.
  • the dry lignite can be introduced into the steam generator, for example, via so-called swirl burners, which are also used in hard coal firing.
  • swirl burners should not be too big. Swirl burners are limited in their size. In general, a thermal power of 60MW is considered technically feasible. For large brown coal boilers with dry lignite auxiliary firing, this requires a correspondingly high number of swirl burners. This leads to high investment costs as a result.
  • Dry lignite is a comparatively low-cost start-up and support fuel for coal-fired steam generators.
  • the vortex burners previously described with regard to their disadvantages are customary, since they ensure a stable flame and a good burnout even in still cold fire spaces.
  • the invention is therefore based on the object to provide a process for the co-incineration of dry lignite in raw lignite-fired steam generators, which takes into account the aforementioned problem.
  • Dry lignite in the context of the invention is to be understood as meaning lignite which has dried from the mined mining product to a dried finished product having a moisture content of 10 to 30% by mass, preferably between 10 and 25% by mass and a mean grain diameter D50 of 0.4 to 10 mm in a drying unit was produced.
  • Mine-wet crude lignite refers to the untreated crushed and optionally pre-shred mined lignite that has a moisture content of between 45 and 65% by mass.
  • Under ground-dried raw lignite is to be understood in a mill with simultaneous drying to a ready-to-burn finished product lignite, of which about 85 to 95 percent by mass has a particle size of less than 1 mm.
  • a burner allocation in the context of the invention is to be understood as meaning a fuel supply line from the mill to a single burner, a burner group or a burner level. Burner allocation ends where the fuel is ignited by supplying combustion air. Burner allocation may include classifiers and distributors.
  • the process of the invention can be summarized in that in the boiler of the steam generator in addition to meal-dried raw lignite dry lignite is mitverbrannt, the dry lignite is the suspension gas / fuel mixture from the mill before the allocation or in the allocation to the individual coal burner abandoned. Unlike a previously practiced process variant, the dry lignite is not burned through separate swirl burner in the boiler, but the dry lignite is added to the flue gas lignite stream of the mill before the boiler.
  • Carrying gas in the context of the invention is to be understood as meaning a mixture of flue gas, evaporated water and combustion air.
  • dry lignite can be redirected from start-up burners of the steam generator to the operated with raw lignite first mill via a switching device as soon as a starting and support firing is no longer needed.
  • the grinding of the raw lignite takes place in inerted with the drying flue gas stream atmosphere.
  • Inertized according to the invention means that the oxygen content in the flue gas drying stream is adjusted to an oxygen content of ⁇ 12% by volume.
  • the dry lignite is fed from the separate drying unit in the first mill and is subjected there to the raw lignite a Nachmahlung.
  • the dry brown coal is subsequently dried in an inertized atmosphere and comminuted.
  • the influence of a The fluctuating moisture content of the dry brown coal is thereby eliminated.
  • moisture, bulk density and grain variations of the dry lignite due to the additional mill drying in mixture with the lignite coal are not critical. This also makes it possible to operate a connected drying unit with optimized performance.
  • the inventive method is favorable in terms of NOx concentration in the flue gas, since by the addition of dry lignite in the flue gas lignite stream concentration of the dust fraction takes place at the burners, so that the Traggasanteil is reduced at the burners. As a result, this leads to a lower NOx concentration in the flue gas / exhaust gas than in a conventional furnace, in which the fuel-related carrying gas amount is usually higher.
  • Another advantage is that the controllability of the furnace is improved. If the amount of raw lignite is increased, the first mill reacts only with a longer dead time, because the mill for the higher amount of coal has to be moved to another operating point, or an additional mill must be put into operation. By contrast, an increase in the amount of dry lignite coal in a relatively short time means that a larger quantity of fuel is available. This improves the controllability of the entire steam generator system.
  • At least one indirectly heated dryer is provided as a separate drying unit.
  • This can be, for example, a fluidized-bed dryer.
  • a second mill is used as a separate drying unit in which drying is carried out in an atmosphere rendered inert by a drying flue gas stream.
  • a drying unit can find application in which the lignite is subjected to direct drying in direct contact with flue gas.
  • the dried lignite from the second mill is fed as dry lignite in the flue gas brown waste stream of the first mill. It can be provided, for example, that the dried lignite from the second mill is completely fed as dry lignite in the flue gas lignite stream of the first mill, so that the second mill is not charged in the usual way unmitelbar the boiler with a flue gas lignite stream.
  • the inventive method is characterized in particular by the fact that the boiler is fired with a tangential firing with jet burners to which the flue gas brown coal stream is allocated. Jet burners are in operation much less susceptible to interference than omnidirectional burners or swirl burners. Jet burners are also structurally much simpler. These are based on the principle that the fuel / carrier gas channel is formed substantially as a rectangular shaft, which is enclosed in each case by corresponding secondary air ducts. A turbulence and twisting of the flue gas / fuel flow or the secondary air flow with corresponding flow dynamics acting internals is not required.
  • the dry brown coal from the separate drying unit is fed into a carrier gas recirculation line of the first mill.
  • Carrying gas recirculation lines are commonly used to control the performance of the mill by, if appropriate, diverting a portion of the carrier gas behind the mill and recirculating it through the mill.
  • the dry brown coal can be fed into a solids return of a mill classifier. Even such a procedure requires hardly any structural adjustments of existing mills.
  • the dry lignite is introduced with at least one screw conveyor in an inlet region of the first mill.
  • an injection of dry brown coal into the first mill with inert gas for example low-pressure steam, or, for example, dry lignite mixed with recirculated carrier gas as the pumped medium. It is expedient to blow dry brown coal in such a way that rapid mixing of the dry brown coal with the raw lignite takes place.
  • the entry point for the dry brown coal may also be provided after the first mill in the burner allocation.
  • a mixture of ground-burnt lignite and dry lignite is to be charged approximately evenly all burners of the boiler, it is advantageous to feed the lignite already in the first mill or in the flue gas lignite stream immediately behind the first mill. In principle, however, it may also be desirable to set a different fuel concentration at firing above the height of the steam generator. In any case, it is favorable for the combustion of the fuel to set a higher fuel concentration at the lower burners, which are considered above the height of the steam generator, than in the case of the upper burners.
  • the dry brown coal is behind the first one Mill and behind a branch of the flue gas lignite stream to a Nachre surgeon or Brüdenbrenner, the flue gas lignite stream for the main burner is added.
  • a concentration of the fuel at the lower burners (main burner) is achieved, so that a low NOx combustion is achieved.
  • impact wheel mills can be used in which takes place in a known manner an impact stress of the ground material.
  • wet fan mills or blower mills can be used.
  • the dry brown coal can be added, for example, in the proposal part of the mill.
  • the indirect drying of the brown coal is carried out in at least one fluidized bed dryer.
  • the energy of the resulting in the indirect drying vapor is at least partially used for preheating the combustion air and / or the boiler feed water.
  • the amount of dry brown coal fed in is regulated as a function of the load of the steam generator.
  • the process flow diagram shown in the figure shows a boiler 1 with a combustion chamber 2 and a convection part 3.
  • the convection part 3 comprises in a known manner heating surfaces, by means of which a convective heat transfer takes place in the heating medium.
  • Within the combustion chamber 2 is dried dust-like lignite burned on dust burners, which are designed as jet burners.
  • the radiant heat is transferred to the circulating in the steam cycle of the boiler 1 heating medium.
  • the steam generated by the boiler 1 can be expanded in a steam turbine to generate electrical energy, alternatively, the steam can also be used as process heat in other coupled processes.
  • the fuel in the form of dry brown coal and raw lignite coal is ground in a beater mill 5 and distributed over a burner allocation 6 on several jet burners.
  • the beater wheel mill 5 on the one hand pit-wet raw lignite 7 and on the other hand dry lignite 8 supplied from a drying unit, not shown.
  • the dry lignite 8 is added either to a carrier gas recirculation line 15 or the beater wheel mill 5 directly.
  • a flue gas lignite stream 10 is supplied to the burner allocation 6, behind the flue gas lignite stream 10 combustion air 11 is added.
  • the combustion air 11 is taken from the atmosphere and preheated via a combustion air preheater 12.
  • the combustion air preheater 12 is operated with the flue gas stream 13 from the convection part 3 of the boiler 1.
  • a portion of the combustion air 11 is added to the drying flue gas stream 9 in front of the beater wheel mill 5, a further part is added to the boiler 1 as burnout air 14.
  • the raw lignite 7 is together with the Dry lignite 8 reground and after-dried and intimately mixed.
  • the flue gas lignite stream 10 (carrier gas stream) leaving the impact wheel mill 5 comprises, for example, about 15% to 35%, preferably about 20% to 25% dry lignite 8 based on the calorific value of the total fuel used at full load of the boiler.
  • the dry brown coal 8 is added to the flue gas brown coal stream 10 behind the impact wheel mill 5, but before the end of the burner allocation 6.
  • the combustion air 11 is preheated by means of the flue gas stream 13 in the combustion air preheater 12.
  • the invention is to be understood that instead of a combustion air preheating 12 with flue gas combustion air preheating is used, which is operated with low-temperature heat from the drying of the dry lignite.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Combustion Of Fluid Fuel (AREA)
  • Air Supply (AREA)

Claims (15)

  1. Procédé de fonctionnement d'un générateur de vapeur avec une chaudière fonctionnant au lignite, avec au moins un premier broyeur pour broyer le lignite, le procédé comprenant les étapes de procédé suivantes :
    - broyage de lignite ayant subi l'humidité de la mine dans le premier broyeur ;
    - branchement d'un flux de gaz de fumée de séchage provenant de la chaudière ;
    - séchage du lignite brut dans le premier broyeur au contact direct du flux de gaz de fumée de séchage ;
    - mise à feu d'un flux de lignite séché par gaz de fumée provenant du premier broyeur dans la chaudière ; et caractérisé par les étapes de procédé suivantes :
    - séchage d'une quantité partielle de lignite brut dans un groupe de séchage séparé pour obtenir du lignite sec ; et
    - amenée du lignite sec provenant du groupe de séchage séparé dans le flux de lignite séché par gaz de fumée du premier broyeur avant une distribution dans le brûleur ou pendant la distribution dans le brûleur.
  2. Procédé selon la revendication 1, caractérisé en ce que le groupe de séchage séparé prévu est au moins un sécheur à chauffage indirect.
  3. Procédé selon la revendication 1, caractérisé en ce que le groupe de séchage séparé prévu est au moins un deuxième broyeur dans lequel le séchage est réalisé au contact du flux de gaz de fumée de séchage dans une atmosphère rendue inerte.
  4. Procédé selon la revendication 3, caractérisé en ce que le lignite séché provenant du deuxième broyeur est intégré au moins en partie sous la forme de lignite sec dans le flux de lignite séché par gaz de fumée du premier broyeur.
  5. Procédé selon la revendication 1 à 4, caractérisé en ce que le lignite sec provenant du groupe de séchage est amené dans le broyeur et y est soumis, conjointement avec le lignite brut, à un post-broyage.
  6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que la chaudière est enflammée avec des brûleurs sans flamme auxquels sont amenés le flux de lignite séché par gaz de fumée.
  7. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que le lignite sec est amené dans une conduite de recirculation de gaz de sustentation du premier broyeur.
  8. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que le lignite sec est amené dans un retour de matière solide du séparateur de broyeur du premier broyeur.
  9. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que le lignite sec est amené dans une zone d'entrée du premier broyeur à l'aide d'au moins un transporteur à vis sans fin.
  10. Procédé selon l'une quelconque des revendications 1 à 9, caractérisé en ce que le premier broyeur utilisé est au moins un broyeur à roue percutante.
  11. Procédé selon l'une quelconque des revendications 1 à 10, caractérisé en ce qu'entre 15 % et 35 % de la totalité du lignite à brûler, par rapport au pouvoir calorifique du lignite en pleine charge du générateur de vapeur, est soumise à un séchage dans un groupe de séchage séparé.
  12. Procédé selon l'une quelconque des revendications 1 ou 2 ou 6 à 11, caractérisé en ce que le séchage indirect du lignite est réalisé dans au moins un sécheur à lit fluidisé.
  13. Procédé selon la revendication 12, caractérisé en ce que l'énergie des vapeurs produites lors du séchage indirect est utilisée au moins en partie pour préchauffer l'air de combustion et/ou de l'eau d'alimentation de la chaudière.
  14. Procédé selon l'une quelconque des revendications 1 à 13, caractérisé en ce que le lignite sec est réacheminé dans le flux de lignite séché par gaz de fumée du premier broyeur par les brûleurs d'attaque du générateur de vapeur au moyen d'un dispositif d'inversion dès qu'un foyer d'attaque et/ou de soutien n'est plus nécessaire pour le générateur de vapeur.
  15. Procédé selon l'une quelconque des revendications 1 à 14, caractérisé en ce que la quantité de lignite sec accumulé est réglée en fonction de la demande de charge de la puissance de combustion du générateur de vapeur.
EP13777007.9A 2012-10-11 2013-10-10 Procédé de fonctionnement d'un générateur de vapeur Not-in-force EP2906876B2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL13777007T PL2906876T5 (pl) 2012-10-11 2013-10-10 Sposób eksploatacji wytwornicy pary

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102012019928.7A DE102012019928A1 (de) 2012-10-11 2012-10-11 Verfahren zum Betrieb eines Dampferzeugers
PCT/EP2013/071139 WO2014057025A2 (fr) 2012-10-11 2013-10-10 Procédé permettant de faire fonctionner un générateur de vapeur

Publications (3)

Publication Number Publication Date
EP2906876A2 EP2906876A2 (fr) 2015-08-19
EP2906876B1 true EP2906876B1 (fr) 2016-12-28
EP2906876B2 EP2906876B2 (fr) 2020-01-01

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EP13777007.9A Not-in-force EP2906876B2 (fr) 2012-10-11 2013-10-10 Procédé de fonctionnement d'un générateur de vapeur

Country Status (7)

Country Link
EP (1) EP2906876B2 (fr)
CN (1) CN104781606B (fr)
AU (2) AU2013328717A1 (fr)
CA (1) CA2887109C (fr)
DE (1) DE102012019928A1 (fr)
PL (1) PL2906876T5 (fr)
WO (1) WO2014057025A2 (fr)

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DE102012019928A1 (de) 2012-10-11 2014-04-30 Rwe Power Aktiengesellschaft Verfahren zum Betrieb eines Dampferzeugers
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EP2906876A2 (fr) 2015-08-19
PL2906876T3 (pl) 2017-06-30
WO2014057025A3 (fr) 2015-01-22
CN104781606A (zh) 2015-07-15
AU2018202163B2 (en) 2019-09-19
WO2014057025A2 (fr) 2014-04-17
CN104781606B (zh) 2017-08-29
EP2906876B2 (fr) 2020-01-01
PL2906876T5 (pl) 2020-07-13
CA2887109A1 (fr) 2014-04-17
DE102012019928A1 (de) 2014-04-30
CA2887109C (fr) 2020-09-01
AU2013328717A1 (en) 2015-05-07
AU2018202163A1 (en) 2018-04-26

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